EP0182309B1 - Verfahren zur hydrierenden Aufarbeitung von Kohlenstoff enthaltenden Abfällen synthetischen bzw. überwiegend synthetischen Ursprungs - Google Patents

Verfahren zur hydrierenden Aufarbeitung von Kohlenstoff enthaltenden Abfällen synthetischen bzw. überwiegend synthetischen Ursprungs Download PDF

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EP0182309B1
EP0182309B1 EP85114535A EP85114535A EP0182309B1 EP 0182309 B1 EP0182309 B1 EP 0182309B1 EP 85114535 A EP85114535 A EP 85114535A EP 85114535 A EP85114535 A EP 85114535A EP 0182309 B1 EP0182309 B1 EP 0182309B1
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Prior art keywords
hydrogen
hydrogenation
process according
oil
waste
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EP85114535A
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German (de)
English (en)
French (fr)
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EP0182309A1 (de
Inventor
Axel Dr. Giehr
Hermann Dr. Höver
Karl-Heinz Dipl.-Ing. Keim
Joachim Dr. Korff
Otto Dr. Neuwirth
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RWE Entsorgung AG
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RWE Entsorgung AG
Union Rheinische Braunkohlen Kraftstoff AG
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
    • C10G1/083—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts in the presence of a solvent
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
    • C10G1/065—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation in the presence of a solvent
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
    • C10G1/086—Characterised by the catalyst used
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

Definitions

  • the present invention relates to a process for working up carbon-containing wastes by hydrogenating them at elevated temperature and a hydrogen pressure of at least 1 bar.
  • waste generated worldwide represents an increasingly greater burden on the environment.
  • waste has been dumped in landfills, e.g. B. stored in abandoned gravel pits, mine pits and other places.
  • landfills e.g. B. stored in abandoned gravel pits, mine pits and other places.
  • the chemical structure of the waste and its long-term effects on soil and groundwater have not been taken into account.
  • certain waste has been stored in so-called special landfills.
  • efforts are made to seal the landfill from groundwater and soil. In the long term, however, there are also dangers to the environment.
  • DE-A-2 211 295 discloses a process according to which cellulose-containing materials can be converted into organic fuel oils with hydrogen in the presence of catalysts such as Fe, Co, Ni, Cu, Ru, Rh, Pd, Ir, Os and Pt .
  • cellulose-containing materials can be converted into a heating oil with hydrogen in the presence of a nickel catalyst, although, as is apparent from the later published publication "Chemical Engineering", January 19, 1987, pages 64 and 65, plastic materials must be removed beforehand and burned.
  • US Pat. No. 4,251,500 describes the hydrogenative cleavage of rubber containing sulfur, in particular old tires, including the tire cord, in the presence of a special catalyst consisting of iron hydroxide, MoO 3 and Cr 2 O 3 , which has a synergistic effect with the sulfur of the rubber vulcanizate .
  • a cobalt molybdate catalyst is also described in US Pat. No. 3,704,108 and "RUBBER AGE", 1974, 106, Vol. 6, pages 27-38, although the tire cord materials must be separated (page 32, right column, 2nd paragraph and p. 29, left column, 2nd paragraph from «RUBBER AGE»).
  • Pyrolysis is now also being used on a technical scale (see, for example, "Venahe dienste GmbH " , October 4, 1985, p. 9).
  • pyrolysis has the disadvantages of the predominant formation of gaseous products and a heavily contaminated coke residue.
  • the hydrogenation of the carbon-containing wastes can be preceded by a stage in which the reaction is carried out with or without a hydrogen donor solvent in the presence of protic solvents, in particular water, at a pressure of 1-150 bar and a temperature of 75-500 ° C and in a second stage at a temperature of 200-600 ° C, preferably 200-540 ° C and at a pressure of 30-500 bar, preferably 50-450 bar.
  • the method according to the invention makes it possible to process synthetic origin wastes from which inorganic constituents such as glass, metals, stone materials and the like have been removed without further sorting to form valuable hydrocarbons, that is to say C 1 -C 4 hydrocarbon gases, in the gasoline sector boiling hydrocarbons and medium and heavy oils that can be used as diesel oil and for heating purposes.
  • pre-sorted materials can in particular be processed in such a way that carbon-containing wastes of synthetic origin, such as plastics or plastic mixtures, rubber, tires, textile wastes, are at least roughly separated from the vegetable or biomass portion and can then be subjected to a hydrating treatment, if necessary together with industrial waste such as B.
  • the synthetic individual components can also be processed very well into valuable liquid products under the conditions according to the invention.
  • the method according to the invention is also very well suited for the joint hydrating treatment of the waste or waste mixtures mentioned with coal, coal components, such as, for example, coal oil residues, coal oils, pyrolysis oils, petroleum, petroleum residues, other petroleum components, oil shale, oil shale components, oil sands, bitumen and the like or the mixtures of these materials.
  • the separation of the above-mentioned inorganic materials from the carbon-containing materials can be carried out according to the prior art. Unless they are reprocessed, these inorganic materials can be deposited.
  • the shredding and separation of waste materials and biomass can also be carried out according to the prior art. Insofar as apparatus conditions do not conflict with this, the process according to the invention can also be carried out in the presence of inorganic materials.
  • Components in waste that are not convertible to hydrocarbons such as B. sulfur, nitrogen, oxygen and halogens in the form of their compounds occur at the hydrogenation reactor outlet as hydrogen compounds in gaseous form, ie as H 2 S, NH 3 , HCl, H 2 0 and others
  • the hydrogenation of the carbon-containing wastes can be carried out with very good results without catalysts. In some cases, even better results with regard to conversion and selectivity of fractions of certain boiling ranges can be obtained in the presence of catalysts, such as, for example, in the presence of Fe, Mo, Ni, Co, W and other hydrogenation-active metals and / or their compounds, these being composed of individual or of at least two of these components can exist and the metals and / or their compounds can be on supports, e.g. B. on aluminum oxide, silicon oxide, aluminum silicates, zeolites and other carriers known to those skilled in the art or of carrier mixtures or also without a carrier. Certain zeolites as such are also suitable.
  • catalysts can be so-called disposable catalysts, such as hearth coke, Winkler gasification dusts, dusts and ashes, which are obtained in the hydrogenating gasification of coal to methane (HKV dusts), Russian such.
  • the catalysts can be pretreated at least in part to sulfide.
  • the temperature is 200-600 ° C, preferably 200-540 ° C
  • the residence time is 1 minute to 8 hours, preferably 15 minutes to 6 hours.
  • Various hydrogen qualities can be used as hydrogenation gas, also with admixtures such as. B. CO, C0 2 , H 2 S, methane, ethane, water vapor, etc.
  • Hydrogen qualities such as those which arise in gasification reactions of carbon-containing materials with water vapor are very suitable. Such materials can be residues from the processing of mineral oils or from coal, wood, peat or residues from the processing of coal, for example hydrogenation. Biomass or the vegetable parts separated from household waste are also suitable.
  • pure H 2 qualities such as hydrogen electrolysis, are also very suitable.
  • domestic waste can first be separated into a vegetable and synthetic portion and then the vegetable portion for hydrogen generation can be gasified while the synthetic portion is subjected to the hydrating treatment.
  • the vegetable portion can also be used for fermentation or other fermentation.
  • the feed product which has generally been largely freed from inorganic materials, optionally dried, comminuted or melted or mixed with grinding oil or other additives, is mixed as such or with a catalyst, brought to the reaction temperature and treated in the reaction zone with hydrogenating gas.
  • a pumpable slurry already forms in the mixing tank at elevated temperature, the feed product can be pumped into the hydrogenation.
  • a so-called grating oil which is produced in the process and can come from various sources in the system, can be added.
  • grinding oil can also be a foreign oil that does not come from the plant.
  • water or steam can also be added.
  • a pumpable slurry can also be created by adding, for example, petroleum components, bitumen or coal components.
  • the feed product can also be used, for example, with the aid of screw conveyors, etc. conveying devices corresponding to the prior art are conveyed into the hydrogenation reactor.
  • the reaction zone can consist of one or more reactors connected in series or in parallel. Downstream of the reactor (s) there is generally at least one hot separator, as is known from the bottom phase hydrogenation, in which separation at the hot separator temperature into gaseous components which are drawn off and into the hot separator sump takes place.
  • the gaseous fractions are cooled, resulting in liquid hydrocarbons which are processed further in accordance with the prior art, for example by means of further hydrogenating cracking stages or refining stages and separation by distillation. In some cases, however, these can also be recycled to grind the input product.
  • the uncondensed gases are freed of H 2 S, NH 3 , HCl, and possibly also CO and CO 2 by gas scrubbing.
  • the hydrogen in the resulting gas can be returned to the hydrogenation reactor (s) as hydrogenation gas.
  • the products from the gas phase of the hot separator in particular the products which are liquid under normal conditions, can, as already stated above, be fed to a refining stage which generally works in a hydrogenating manner. Small amounts of compounds containing heteroatoms which are still present can be worked up completely by hydrogenation, so that the products are then practically sulfur, nitrogen and halogen-free. Higher-boiling fractions can be fed to at least one cracking plant, in particular a hydrocracking plant. If necessary, certain portions of the processing can be returned to the waste hydrogenation or before the waste hydrogenation.
  • Hot separator sump can be worked up in various ways, e.g. B. by vacuum distillation, the bottom of the vacuum distillation gasification to H 2 and CO can be supplied.
  • the gases formed during the gasification are advantageously integrated into the gas scrubbing and gas processing described above.
  • the vacuum distillation residue can also be coked or deasphalted or processed further using other prior art processes.
  • the residues and ashes obtained contain the metallic impurities, which can be landfilled in accordance with the prior art, but they can also be recycled to the metals of the metallurgical industry or, if appropriate, used as catalysts in waste hydrogenation.
  • the hot separator sump or residue can also be subjected to a supercritical extraction, such as. B.
  • the hot separator sump can also be used as a grinding oil, as can the vacuum distillation residue, especially after deasphalting.
  • the method according to the invention is shown by way of example in FIG. 1 with exemplary subsequent steps.
  • FIG. 2 shows an example of the method according to the invention with an upstream solvent treatment.
  • FIG. 3 shows the combination of waste oil refining with the process according to the invention.
  • FIG. 4 shows the dependence of the yields on the individual fractions as a function of the temperature.
  • reactors (5) instead of reactors (5), several reactors can also be used.
  • the hydrogenated product passes from (5) into the hot separator (6).
  • products (7) which are gaseous at the temperature of the hot separator and which reach the separator (9) via heat exchangers (8).
  • (9) the products that are liquid after cooling are drawn off, while the gaseous products escape overhead.
  • the liquid products are worked up in a conventional manner, such as. B. by distillation or, if necessary, hydrogenative cleavage of the heavier oil fraction or by refining.
  • the gases in (10) are freed from admixtures of H 2 S, NH 3 , HCl, C0 2 and others. Hydrogen is circulated and returns to or into the hydrogenation reactor. Gaseous hydrocarbons can also be separated off and some or all of the hydrocarbons can be converted into H 2 and CO by steam reforming (11).
  • the liquid product is drawn off from the hot separator sump and, for example, fed to a vacuum distillation (12). Further oils (13) are obtained there, which can also be used as rubbing oil.
  • the bottom of the vacuum distillation can, for example, be coked in (14).
  • the products (15) withdrawn from the coking overhead are also processed in the gas and liquid product of the plant.
  • the resulting coke (16) which also contains the ash constituents including metals, can get into a gasification (17) or can be deposited according to the state of the art or partially used as a catalyst, depending on the composition.
  • the vacuum distillation sump can be gasified directly in (17).
  • the resulting gases (18) get into the gas processing of the system, while the ash (19) or the soot can be deposited or burned or further processing, eg. B.
  • the metallurgical industry can be supplied or partially used as catalysts, depending on the composition.
  • the contents of the hot separator can be extracted with a supercritical gas.
  • Propane, butane, naphtha cuts, but also hydrocarbon cuts with a higher boiling point are suitable for this.
  • the extract is processed in the usual way.
  • the remaining residue can be processed like the hot separator sump or residue.
  • the extractant can, in particular in the case of a plurality of hydrogenation reactors connected in series, already be introduced at least partially into the reactors themselves.
  • the liquid product from separator (9) can first be subjected to refining (20), generally a hydrogenating refining.
  • refining (20) generally a hydrogenating refining.
  • the refined product goes to a distillation (21), but the distillates can also be refined.
  • the bottom of the distillation can be split in a cracking stage (22) to give lower-boiling products (23).
  • FIG. 1 The processing represented by FIG. 1 is exemplary and does not limit the hydrogenating processing of waste according to the invention, since the prior art for products from hydrogenation reactors comprises a large number of variants.
  • Waste oils or residues from waste oil processing can also be used in the hydrating treatment of waste, as shown in FIG. 3 by way of example.
  • Used oil can be used, for example, from a storage tank (1) in a physical and / or chemical separation or cleaning system (2) in order to separate solid substances, water and the like.
  • the product pre-cleaned in this way can be used via (3) in the hydrogenation reactor (4) or in the refining (7).
  • Gaseous or liquid products from the hot separator (5) of the hydrogenation can be added to (6) the waste oil refinery (7).
  • the bottoms from the distillation (8) of the refined waste oil can also be used in (4) via (9).
  • Waste to be hydrogenated is removed from storage (10) and first goes to a comminution and mixing container (11), from which the feed product is used via (12) in (4).
  • Heavy mineral or coal-derived oils can be added via (13), for example.
  • the hot separator sump or residue can be inserted into gasification (15), for example, via (14).
  • a solvent treatment with suitable solvents in particular hydrogen-transferring solvents or extraction solvents, can precede the hydrogenating treatment, then either the entire mixture consisting of dissolved and undissolved can be fed to the hydrogenation reactor or there is a separation into the dissolved and undissolved behind the dissolving apparatus instead of and solution or undissolved are fed to the hydrogenation reactor (s).
  • the solvent can be recycled in a conventional manner by subsequent distillation.
  • the separated, undissolved solid can also be fed to gasification or coking.
  • the feed product can be mixed with coal and / or coal components and / or petroleum residues and / or petroleum and the like. a., are hydrogenated.
  • Suitable solvents are e.g. B. tetralin, anthracene oil, isopropanol, cresol-containing oils, decalin, naphthalene, tetrahydrofuran, dioxane, but also, for example, petroleum-derived, coal-derived or from the plant itself hydrocarbons and oils and oxygen-containing hydrocarbons and oils. Finally, water and steam can also be added.
  • the hydrogenation product can be worked up in a conventional manner, e.g. B. by distillation (6).
  • wastes can be converted, if necessary in a mixture with biomass, and optionally in a mixture with coal and mineral materials, such as petroleum residues, with high yields of distillable oils.
  • Suitable conditions in the resolution level are 380-480 ° C.
  • the hydrogenation stage is generally carried out at 350-450 ° C. and a pressure of 110-250 bar, preferably of 120-220 bar, it being possible to use the customary hydrogenation catalysts.
  • H-oil process HRI Inc. and Texaco Development Corp.
  • Canmet process Partec Lavalin Inc./Petro Canada
  • the LC-finishing process Limus Crest . Inc.
  • VEBA Veba combi cracking process
  • VEBA LO cracking process VEBA
  • RCD Unibon process UOP Process Division Research Co./UOP, Co.
  • residfining process Exxon Research and Engineering Co.
  • the unicracking and unicracking / HDS process Union Oil of California
  • the HC Unibon process UOP Process Division of UOP Inc.
  • the isocracking process Chevron Research Co.
  • the heavy oil cracking process Phillips Petroleum
  • the Dynacracking process Hydrocarbon Research Inc.
  • the Linde hydroconverter process u. a.
  • At least dissolved waste such as e.g. B. in coal oil and petroleum or their components, treated according to the invention hydrogenating.
  • waste mixtures can also be processed in a hydrogenating manner in such a way that mixtures of vegetable and synthetic waste, if appropriate with the addition of biomass, are reacted in various stages under conditions in which, on the one hand, the hydrolytic and hydrating conversion of vegetable or paper components and biomass Share and on the other hand, the hydrogenation of the synthetic organic waste takes place. Both stages can also be carried out in the presence of a hydrogen donor solvent.
  • a hydrogenating treatment can optionally be carried out in the presence of hydrogenation catalysts and a pressure of 1 bar to 150 bar, preferably 25-60 bar, preferably in In the presence of water and other protic solvents such as alcohols.
  • oils obtained predominantly from the vegetable portion can be separated by solvent extraction, after which the portion not split by hydrogenation can also be split by hydrogenation in the second stage under the conditions already described.
  • the stepwise processing can also be carried out in such a way that vegetable parts or paper parts or biomass are hydrolytically split in the first step, for example in the presence of alkalis or acids, this reaction possibly taking place in the presence of CO and preferably in the presence of water and / or other protic solvents such as alcohols and in the second stage the synthetic or predominantly synthetic portion is reacted in a hydrogenating manner.
  • waste and / or the biomass can be separated into a vegetable portion and a synthetic portion and processed separately under the conditions described.
  • Steps in the present invention are to be understood in such a way that a certain step, such as the above-mentioned first step for hydrolytic degradation of the vegetable portion, can itself consist of several steps connected in parallel or in series.
  • Polystyrene increases the amount of aromatics. With the plastic waste mixtures used, the aromatic content was approx. 25% by weight.
  • Table 2 summarizes the results of the hydrogenation treatment of the synthetic fraction obtained in a waste separation plant with a fraction of 15% by weight of chlorine-containing polymers as a function of the hydrogenation period at 450.degree.
  • the pressure was 200 bar (cold).
  • a used machine oil was used as the mixing component in relation to the waste of 1: 2.3. It was worked without a catalyst.
  • Table 2 shows that at constant temperature, the yield of hydrocarbons with a boiling point ⁇ 180 ° C. increases from 4% by weight (2 hours) to 65% by weight (6 hours), while the proportion of the high-boiling fraction with a boiling range> 390 ° C decreases from 21% by weight to 1% by weight. If the fraction with boiling range 180-390 ° C is used as «own oil», in a mixture with waste feed, the own oil is also converted almost quantitatively to low-boiling hydrocarbons.
  • the halogen content in the product fractions can be eliminated almost quantitatively ( ⁇ 1 ppm) by means of a downstream hydrogenating refining.
  • the entire hydrocarbon product can also be hydrogenated as such.
  • a hydrocarbon fraction with a content of 2400 ppm chlorine obtained from synthetic waste from a green bin and boiling between 180 to 390 ° C. was subjected to a hydrogenative refining at 50 bar hydrogen pressure and 270 ° C. Chlorine was no longer detectable in the product obtained.
  • FIG. 4 shows the dependence of the yield on the individual fractions as a function of the temperature with a residence time of 2 hours.
  • Tables 3 and 4 show results which were obtained in the hydrogenation of a mixture of synthetic waste components, including PVC, from a daily sample of a waste separation plant which contained 10-50% by weight of a vegetable component and a mixture of synthetic waste with 20 to 60% by weight.
  • Waste paper A pressure of 200 bar and a residence time of 4 hours were used at 450 ° C. without catalysts.
  • a vacuum distillate from a coal hydrogenation in the ratio waste to VD of 3: 1 was used. In addition to the specified products, water not recorded in the tables was formed.
  • Table 5 shows the conversion and yield as a function of catalysts.
  • the work was carried out at 450 ° C., 200 bar pressure and 4 hours dwell time.
  • a used spindle oil was used as the admixing component in a ratio of spindle oil to waste of 1: 2.
  • the synthetic organic part of a waste separation plant was used as waste.
  • the conditions were chosen to compare with the previous tables. However, similar results are obtained when the conditions are varied.
  • the table shows that very high conversions can also be achieved by hydrogenation catalysts such as Ni / Mo / aluminum silicate, with a high proportion of fractions with a boiling range below 390 ° C. being obtained at the same time.
  • Iron and nickel catalysts can be used, in particular, to obtain a high proportion of compounds in the boiling range 180-390 ° C.
  • catalysts such as hearth coke and FeS0 4 can be used to obtain a high proportion of compounds in the boiling range ⁇ 180 ° C.
  • waste incineration plants which have a high CO 2 load and pyrolysis plants in which large amounts of gases are generated
  • valuable liquid products are produced in the present invention, so that recycling of consumer products is ensured in an excellent manner.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Wood Science & Technology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Organic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Carbon And Carbon Compounds (AREA)
  • Nitrogen And Oxygen Or Sulfur-Condensed Heterocyclic Ring Systems (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Treatment Of Sludge (AREA)
  • Coke Industry (AREA)
EP85114535A 1984-11-22 1985-11-15 Verfahren zur hydrierenden Aufarbeitung von Kohlenstoff enthaltenden Abfällen synthetischen bzw. überwiegend synthetischen Ursprungs Expired EP0182309B1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT85114535T ATE44756T1 (de) 1984-11-22 1985-11-15 Verfahren zur hydrierenden aufarbeitung von kohlenstoff enthaltenden abfaellen synthetischen bzw. ueberwiegend synthetischen ursprungs.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE3442506 1984-11-22
DE19843442506 DE3442506A1 (de) 1984-11-22 1984-11-22 Verfahren zur aufarbeitung von kohlenstoff enthaltenden abfaellen und biomasse

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EP0182309A1 EP0182309A1 (de) 1986-05-28
EP0182309B1 true EP0182309B1 (de) 1989-07-19

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EP (1) EP0182309B1 (el)
JP (1) JPS61159489A (el)
CN (1) CN1005778B (el)
AT (1) ATE44756T1 (el)
AU (1) AU583865B2 (el)
BR (1) BR8505890A (el)
CA (1) CA1294236C (el)
DD (1) DD249036B5 (el)
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DK538285D0 (da) 1985-11-21
CN85109131A (zh) 1986-10-01
PT81533A (en) 1985-12-01
ES549197A0 (es) 1986-11-16
ATE44756T1 (de) 1989-08-15
BR8505890A (pt) 1986-08-12
DE3442506A1 (de) 1986-05-22
ZA858721B (en) 1986-07-30
PT81541A (en) 1985-12-01
EP0182309A1 (de) 1986-05-28
CN1005778B (zh) 1989-11-15
DE3571637D1 (en) 1989-08-24
NZ214280A (en) 1989-04-26
ES8701207A1 (es) 1986-11-16
DK538285A (da) 1986-05-23
DE3442506C2 (el) 1987-04-16
AU583865B2 (en) 1989-05-11
DD249036B5 (de) 1997-03-20
CA1294236C (en) 1992-01-14
GR852797B (el) 1986-03-19
JPS61159489A (ja) 1986-07-19
PL256375A1 (en) 1987-03-09
PT81533B (pt) 1987-11-11
FI854502A (fi) 1986-05-23
HU193138B (en) 1987-08-28
FI854502A0 (fi) 1985-11-15
NO854663L (no) 1986-05-23
YU181185A (en) 1987-10-31
HUT38601A (en) 1986-06-30
AU5030085A (en) 1986-05-29

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